Process for producing lithium carbonate from concentrated lithium brine

ABSTRACT

Disclosed are methods for a simplified process for preparing lithium carbonate from concentrated lithium brine which can be used for battery grade, pharmaceutical and other high purity grade applications. Impure lithium carbonate is precipitated from lithium concentrated brine, preferably lowered in magnesium, subsequently suspended in aqueous solution and reacted with carbon dioxide to form dissolved lithium bicarbonate. The insoluble impurities are filtered and the dissolved boron and metal impurities such calcium, magnesium and iron are physically separated from the lithium bicarbonate solution using ion selective mediums or other selective processes. Lithium carbonate is then subsequently precipitated.

FIELD OF THE INVENTION

The present invention relates to an efficient and simple process for theproduction of lithium carbonate of high purity, from natural orartificial brines which normally have values of boron, calcium,magnesium, sulfates among others.

BACKGROUND

Although lithium is widely distributed on Earth, there are very fewcommercial sources where lithium is found in concentrated valuessuitable for producing lithium compounds. One main source is the mineralspodumene, which is a double lithium-aluminum silicate, LiAl(SiO₃),which has a theoretical lithium content of 8.03%. Other minerals whichare exploited are petalite, LiAl(Si₄O₁₀), which has a theoreticalcontent of Li₂O of 4.88%, and lepidolite, which has a variablecomposition represented by the formula K₂(LiAl)₃(SiAl)₄O₁₀(OH,F)₂.Another mineral of high potential value for obtaining lithium ishectorite, which is a low grade mineral with the compositionNa_(0.33)(Mg,Li)₃Si₄O₁₀(OH,F)₂ and which is not yet exploited foreconomic reasons.

Other sources for obtaining lithium, which have grown in importance inthe last two decades, are the brines from salars, salt lakes, salt minesand geothermal resources. The highest lithium concentrations are foundin salar deposits, which actually supply the majority of lithium toindustry. The elements of major economic interest in salar type saltsystems are lithium, potassium and boron. Important parameters forprocess development are:

-   -   a) the initial lithium concentration;    -   b) the Mg/Li ratio which reflects how much magnesium has to be        removed by fractional crystallization or selective        precipitation;    -   c) the Ca/Li ratio which indicates how much calcium has to be        removed by fractional crystallization or selective        precipitation;    -   d) the SO₄/Li ratio which indicates whether the deposit is a        lithium sulfate deposit (high SO₄/Li) or a lithium chloride        deposit (low SO₄/Li). With a high ratio, lithium sulfate salts        start to precipitate at lithium concentrations typically between        0.5% to 1%.

In an evaporation process, calcium will concentrate together withmagnesium and both have to be removed before lithium carbonate can beprecipitated. When calcium concentrations are high, sulfateconcentrations are low. Some typical components of naturally occurringbrines are identified in the Table I below.

TABLE I Saline Brine Analysis (mg/l) Resource Li K Mg Ca SO4 B Mg/LiSO4/Li Ca/Li Salar de Atacama Average 1,835 22,626 11,741 379 20,180 7836.4 11.0 0.2 Salar Salinas Grandes 775 9,289 2,117 1,450 1,036 232 2.71.3 1.9 Salar de Hombre Muerto 744 7,404 1,020 636 10,236 420 1.4 13.80.9 Salar de Hombre Muerto East Side 745 8,318 1,781 8,642 2.4 11.6 —Silver Peak 245 5,655 352 213 7,576 85 1.4 30.9 0.9 Salar de Olaroz(production wells) 774 6,227 2,005 416 18,630 1,136 2.6 24.1 0.5 Salarde Cauchari 618 5,127 1,770 476 19,110 1,360 2.9 30.9 0.8 Salar de UyuniAverage 424 8,719 7,872 557 10,342 242 18.6 24.4 1.3 Salar de Rincon 3977,513 3,419 494 12,209 331 8.6 30.7 1.2 Salar de Maricunga 1,036 8,8698,247 11,919 1,095 634 8.0 1.1 11.5

In the case of low Mg/Li brines, such as at Silver Peak, a process canbe used in which magnesium is removed with slaked lime from, fresh wellbrine or brine which is primarily concentrated in solar evaporationponds. After the magnesium removal, the brine is concentrated toapproximately 0.6% to 0.7% wt Li/wt brine, because at a higherconcentration lithium sulfate salts will begin to precipitate. Duringthe solar evaporation process principally sodium chloride together withsome glaubersalt (Na₂SO₄.10H₂O), glaserite (Na₂SO₄.3K₂SO₄) and gypsum(CaSO₄.2H₂O) are crystallized. In the more concentrated ponds, silvinite(KCl.NaCl) salts crystallize, which is feedstock for the production ofpotassium chloride (KCl). The concentrated lithium brine is purified bya boron removal step. The removal step can be completed by the additionof a mixture of calcium chloride and slaked lime, by solvent extractionof boric acid or by a brine polishing stage. The remaining magnesium andcalcium are removed from the brine by adding (i) caustic soda or sodiumash, (ii) a recycled lithium carbonate end liquor, (iii) a mixture ofslaked lime and soda ash or (iv) a combination of any two of more of(i)-(iii). Subsequently, the brine is filtered and heated between 60 to90° C. and a soda ash solution is added to precipitate lithiumcarbonate. The precipitated lithium carbonate is filtered washed anddried. This process produces a technical grade lithium carbonate(typically 99.0% wt Li₂CO₃) which is not suitable for the more exigentlithium battery industry or for pharmaceutical compositions that containlithium carbonate.

At the Salar de Hombre Muerto, which is also a low Mg/Li brine, thebrine is conditioned to the appropriate pH and temperature before itenters a sorption-desorption process where lithium, as lithium chloride(LiCl), is selectively recovered. The pregnant liquor containsapproximately 0.16% wt Li/wt brine. Afterwards, the effluent is sent tothe solar evaporation ponds where it is purified, concentrated and pHadjusted. If the brine reaches a concentration of 3% % wt Li/wt brine,it is sent to the lithium carbonate process, where boron is removed withselective ion exchange. The remaining magnesium and calcium are removedfrom the brine with the addition of (i) sodium hydroxide and sodiumcarbonate, (ii) recycled lithium carbonate end liquor, (iii) a mixtureof slaked lime and soda ash or (iv) a combination of any two or more of(i)-(iii). The brine is filtered and heated between 60 to 90° C. and asoda ash solution is added to precipitate lithium carbonate. Theprecipitated lithium carbonate (typically 99.5% wt Li₂CO₃), is filteredwashed and dried. This process produces a battery grade of midrangepurity.

The brines with higher Mg/Li ratios, such as at the Salar de Atacama,are pumped from the salar reservoir and are evaporated in large shallowpools, where a sequential crystallization of the salts commences. As thechloride brines are generally saturated with sodium chloride, the firstsalt to be precipitated is halite with some gypsum, followed bysilvinite . crystallization. Further evaporation leads to carnalite(KCL.MgCl₂.6H₂O) and then bischofite (MgCl₂.6H₂O) crystallization. Atthis stage, the lithium is increased to about 30 4.5% wt Li/wt brinewith a magnesium content of about 4%. The evaporation of the brinecontinues forcing the crystallization of lithium carnalite(LiCl.MgCl₂.6H₂O), which is leached with less concentrated brine torecover part of the lithium content. The final lithium chloride brinecontains about 6% wt Li/wt brine, 1.8% wt magnesium/wt brine, 0.8% wtboron/wt brine and some minor amounts of potassium, sodium and sulfate.Subsequently, the boron is removed as boric acid by solvent extraction.After the boron extraction, the brine is mixed with the lithiumcarbonate plant end liquor in order to precipitate most of the magnesiumas magnesium carbonate. The brine is filtered and sent to the secondstage of magnesium and calcium removal. In this second stage, a mixtureof slaked lime and soda ash is added to the filtered brine in order toprecipitate the magnesium as magnesium hydroxide and the calciumprecipitates as calcium carbonate. The resulting sludge is filtered andthe purified brine is sent to the lithium carbonate stage. Soda ashsolution is added to the purified lithium brine in order to precipitatelithium carbonate. This reaction takes place at elevated temperaturesnormally between 60 to 90° C. Subsequently, the lithium carbonate(typically 99.4% wt Li₂CO₃), is filtered and the cake washed on a beltfilter and finally dried. This process produces a battery grade of lowrange purity.

New brine deposits, with low Mg/Li and low sulfate brines (low SO₄/Li),such as Salinas Grandes or relatively low sulfate brines as at the EastSide Salar de Hombre Muerto, the lithium can be concentrated up to 6% wtLi/wt brine. Other brine deposits with high Mg/Li and high SO₄/Li, suchas the sulfate brine in the Salar de Atacama, Salar de Uyuni, East andWest Tanjinair Salt Lakes in China, and those with high Ca/Li brinessuch as Salar de Maricunga in Chile currently lack industrialapplication. Nevertheless, various process developments attempt togenerate concentrated lithium brines suitable to precipitate lithiumcarbonate.

One process development involves using an additional process in which animpure feed of lithium carbonate (Li₂CO₃) is mixed with an aqueoussolution and reacted with CO₂, preferably under pressure, to producedissolved aqueous lithium bicarbonate (LiHCO₃). Insoluble impuritiessuch as iron, magnesium and calcium are removed by physical means suchas filtration or centrifugation. Soluble divalent or trivalent ions suchas magnesium, calcium and iron are adsorbed by selective ion exchange orother similar methods. Carbon dioxide is then completely or partiallyremoved by raising the solution temperature and/or releasing thepressure to enable pure Li₂CO₃ to precipitate. A part of the solution isreturned to the bicarbonation reaction zone to enhance the economics ofthe process. Undesirable impurities remain in solution.

Although there are many ways to produce lithium carbonate from lithiumcontaining brine, no simplified process exists to produce lithiumcarbonate of high purity, such as battery or pharmaceutical grade, fromconcentrated lithium brines that contain significant amounts of othervalues such as boron, magnesium, calcium, sodium, potassium, chlorideand sulfate. Typical values for battery grade or pharmaceutical gradelithium carbonate are shown in Table II.

TABLE II Typical values for Battery Grade or Pharmaceutical GradeLithium Carbonate Battery Grade Battery Grade Pharmaceutical (low)(high) Grade Li₂CO₃ 99.20 99.60 99.70 Na 0.060 0.018 0.003 Fe 0.0020.0001 0.0003 Ca 0.040 0.005 0.01 SO4 0.100 0.020 0.01 K 0.010 0.00040.001 Cl 0.010 0.002 0.001 H2O 0.400 0.193 0.05 Mg 0.010 0.002 0.001 Cr0.0010 0.0002 ND Ni 0.0030 0.0002 ND Cu 0.0010 0.0002 ND Pb 0.002 0.002ND Heavy Metal (Pb) 0.0020 0.0020 0.0002 As ND ND 0.0002 Al 0.005 0.0003ND Zn 0.005 0.0007 ND B 0.001 0.0002 ND Mn 0.0005 0.0003 ND Si 0.0050.0010 ND F 0.010 0.0050 ND Insol. In HCl 0.0030 0.0020 0.00 LOI (550°C.) 0.010 0.0050 ND ND = No Data available

SUMMARY OF THE INVENTION

According to one embodiment of the present invention there is provided amethod of producing lithium carbonate, comprising the steps of:

-   -   a) precipitating impure lithium carbonate from an impure lithium        containing brine by addition of soda ash;    -   b) reacting the precipitate of impure lithium carbonate in a        first aqueous solution with CO₂ to form a second aqueous        solution containing dissolved LiHCO₃ and dissolved impurities        and insoluble impurities from said impure lithium carbonate;    -   c) separating said insoluble impurities from said second aqueous        solution;    -   d) separating said dissolved impurities from said second aqueous        solution by contacting said dissolved impurities with one or        more ion selective mediums to remove said dissolved impurities        wherein at least one of the ion selective mediums removes boric        acid and/or borates; and    -   e) precipitating Li₂CO₃ from said second aqueous solution.

BRIEF DESCRIPTION OF FIGURES

The accompanying drawings show an illustrative flow sheet of the processof the present invention and solubility graphs of lithium expressed as alithium carbonate equivalent in the lithium bicarbonation process.

FIG. 1 schematically illustrates a flowchart of the possible stepsinvolved in the present invention.

FIG. 2 is a graph of total concentration of Li₂CO₃ that can besolubilized as LiHCO₃ as a function of the pressure CO₂ at particulartemperatures. Data points labeled as ‘Seidell’ are taken from page 385of Volume II of Solubilities, Inorganic and Metal Organic Compounds: Acompilation of solubility data from the periodical literature, gatheredby Atherton Seidell and William F. Linke, 4th edition, published by VanNostrand, 1958 (Data points labeled ‘Orocobre’ in FIG. 2 are dataacquired by autoclave lab scale solubility tests that were performed atthe test facilities installation of the company SGS Group in Lakefield,Canada. The labels display the temperature conditions of either theOrocobre experiments or the temperature conditions published by Seidelland Linke. FIG. 2 includes only one data point corresponding to theOrocobre solubility test conducted at 6° C. and 6 atm).

FIG. 3 is a graph of total concentration of Li₂CO₃ at particulartemperatures after temperature rise and and/or pressure release in orderto desorb CO₂. The labels next to the solubility points indicate thebicarbonation conditions such as temperature and pressure.

At the right side of the label the precipitation conditions areindicated, such as vacuum application (vac), air sparging (air) or ionexchange (IX) treatment.

DETAILED DESCRIPTION

In order to fulfill battery grade and pharmaceutical gradespecifications, processes for lithium carbonate production will likelyrequire a purification process that employs a lithium bicarbonationstep. The present invention avoids the costly and complex boron removalstep prior to lithium carbonate precipitation, by a simple ion exchangeboron removal step in the recrystallization process. The amount of boronthat needs to be removed by the process of the invention is only afraction of the amount that needs to be removed when using a solventextraction process, as only a portion of the boron co-precipitates withimpure lithium carbonate when using the process of the presentinvention. For example, approximately 600 mg boron/kg Li₂CO₃ may onlyneed to be removed when using the process, of the present invention,whereas an amount of approximately 25,000-124,000 mg boron/kg Li₂CO₃needs to be removed when using a process that includes a solventextraction step to remove boron.

The present invention provides an efficient and economical process forthe production of battery grade or pharmaceutical grade lithiumcarbonate from concentrated lithium containing brine with concentrationsbetween 0.4% to 6.5% wt Li/wt brine, depending on the brine source. Theimpure brine is heated to a temperature between approximately 20 and100° C. and, preferably, the amount of magnesium in the brine isreduced. Successively, a 15%-30% w/w soda ash solution is added to thefiltered brine in order to precipitate impure lithium carbonate, whichis then filtered and washed. The impure lithium carbonate is mixed withcooled mother liquor from a bicarbonation process. The slurry is sent toa reactor where it is reacted with a stoichiometric excess amount of CO₂with respect to LiHCO₃, preferably under pressure between 0.7 and 20atm, and between a temperature of approximately −12 to 40° C. to producean aqueous solution with dissolved LiHCO₃. The lithium bicarbonatesolution is filtered in order to remove the insoluble impurities, suchas silica, iron, magnesium and calcium compounds. Soluble or partiallysoluble ions such as magnesium, calcium and other dissolved ions such asFe, Ni, Cr, Cu, Pb, Cd, Al, Zn, Mn, Si and boron can be adsorbed byselective ion exchange resins or other similar methods. Otherundesirable impurities such as Na, K, Cl and SO₄ remain in solution.Carbon dioxide is then completely or partially removed by raising thesolution temperature between approximately 20 and 100° C. and/orreleasing the pressure. By removing CO₂, Li₂CO₃ of battery grade orpharmaceutical grade precipitates, which is then filtered, washed anddried. The dried product is micronized according to size specifications.One fraction of the mother liquor resulting from the final precipitationstep is returned to the bicarbonation reaction zone, another fraction issent to wash the impure lithium carbonate obtained from the initialprecipitation step to enhance the economics of the process.

The process of the invention will now be described with reference to theFigures. FIG. 1 schematically illustrates a flowchart of one embodimentof the present invention The concentrated lithium brine designated asstream (1) in FIG. 1, is the raw material for the process and variesbetween approximately 0.4% and 6.5% wt Li/wt brine depending on thesource of the lithium containing brine and the process by which thebrine is concentrated. If the magnesium levels in the brine are high,for example above 200 mg/l, magnesium can be removed beforeconcentrating the brine, or the magnesium can be removed as magnesiumhydroxide after the brine is concentrated but before precipitatingimpure lithium carbonate. The removal of magnesium as magnesiumhydroxide can be done, for example, by the addition of (i) lithiumcarbonate plant end liquor (24) (ii) caustic soda, (iii) a mixture ofslaked lime and soda ash or (iv) a combination of any two or more of(i)-(iii). In this case the brine has to be filtered to remove themagnesium hydroxide. The precipitation of magnesium hydroxide ispreferably done at elevated temperatures between approximately 40 and100° C.; by heating the brine designated as stream (2) in FIG. 1 usingone or more heat exchangers (A). The precipitation of magnesiumhydroxide occurs in a vessel (B) that is preferably slightly agitated.Co-precipitation of calcium carbonate may also occur at this stage. Thebrine (4) is then filtered with a solid liquid separation device (C)such as a press filter or a polishing filter. The filtrate (5) is heatedto a temperature of between approximately 60 to 90° C. +(20° C.). In oneembodiment, a soda ash solution (6) is added to the heated brine in oneor more various agitated reactors (D) in order to precipitate impurelithium carbonate. Subsequently, the lithium carbonate pulp (7) isfiltered and washed with mother liquor (19) from a bicarbonation processin a solid liquid separation device (E), preferably a belt filter or apeeler centrifuge. The lithium carbonate (8) is mixed in an agitatedvessel (F) with a mixture of weak filtrate (mother liquor) and strongfiltrate (18). This mixture (9) is fed to a bicarbonation reactor (G) ata temperature between approximately −15 to 40° C., preferably 0 to 25°C.±15° C., more preferably 5 to 15° C.±5° C., together with a carbondioxide stream (10 & 16) at a pressure between 0.7 atm and 20 atm, butpreferably between 1 and 8 atm for temperatures between about 0° C. andabout 10° C. or between 8 and 15 atm for temperatures between 10 and 40°C. Bicarbonation can be carried out with an excess of carbon dioxide ofup to 10 times the stoichiometric amount. For example, an excess of thestoichiometric amount of CO₂ with respect to LiHCO₃ can be between 1 and10, preferably between 1 and 2, more preferably between 1 and 1.3. Underthese conditions, dispersed lithium carbonate is transformed intolithium bicarbonate (LiHCO₃) soluble in the aqueous solution accordingto the following reaction.

Li₂CO₃(s)+H₂O(I)+CO₂(g)⇒2LiHCO₃(aq)   (reaction scheme a)

Impurities such as iron, calcium and magnesium remain either totallyinsoluble or partially insoluble after bicarbonation. The maximumsolubility of LiHCO₃ expressed as lithium carbonate equivalent isincreased at lower temperature and at higher partial pressure of carbondioxide in the vessel as can be observed, in FIG. 2. A slight excess ofcarbon dioxide is preferred to ensure complete dissolution of thelithium carbonate. The solution containing the dissolved lithiumbicarbonate (11) is fed through a solid liquid separation device (H)such as press filter or a polishing filter at the same pressure as usedduring the bicarbonation reaction to remove insoluble or partlyinsoluble compounds such as iron, calcium, magnesium, carbonates,hydroxides and borates as well as silicate and aluminate species. Forexample in the case where there is significant presence of magnesiumand/or calcium the filtered solution (12) can then be fed to one or moreion exchange columns (I) or other selective method, such asliquid-liquid extraction that employs:

-   -   a) one type of resin or fiber with an aminophosphonic acid        functional group (—CH2-NH—CH2-PO₃Na₂) such as, but not limited        to, AMBERLITE™ IRC747, Purolite S-940, Purolite S-950, Durolite        C-467; and/or with a iminodiacetic acid functional group such        as, but not limited to, AMBERLITE™ IRC748, Lewatit MonoPlus TP        207 and Purolite S-930 in order to remove one or more of the        following magnesium, calcium and other ions such as Fe, Ni, Cr,        Cu, Cd, Pb, Al, Zn, Mn, As and Si present in trace quantities;        and/or    -   b) one type of resin or fiber with a N-methyl-glucamine        functional group, such as, but not limited to, AMBERLITE™        IRA743, AMBERLITE™ PWA10, Purolite S108 and Purolite S110,        Lewatit MK in order to remove boric acid and borates from        filtered solution (12).

The purified lithium bicarbonate solution (13) having low levels of Mg(<100 ppm), Ca (<20 ppm) , B (<100 ppm), Fe (<20 ppm) and otherdissolved ions (all less than <20 ppm) is heated in a vessel (J) to atemperature of approximately 50 to 70° C.±20° C., more preferably 60 to80° C.±10° C., even more preferably 65 to 75° C.±5° C. to precipitatelithium carbonate as can be seen in FIG. 3 and at a pressure that isless than the pressure applied in the bicarbonation reaction. Thepressure applied can be between vacuum and 20 atm, but preferablybetween vacuum and 1 atm. As the lithium carbonate is precipitated, thecarbon dioxide is released from vessel (J) which is preferably agitated,according to reaction scheme (b) shown below.

LiHCO₃(aq.)⇒Li₂CO₃(s)+H₂O(1)+CO₂(g)   (reaction scheme b)

The released carbon dioxide is evacuated through line (15), by a carbondioxide recovery system (N) where it is cooled, dried and recompressedfor reuse in the bicarbonation reactor. Alternatively, it can bereleased to the atmosphere.

Under these conditions, pure lithium carbonate (>99.6%) precipitates,whereas ions such as sodium, potassium and sulfate remain soluble in thesolution. The pure lithium carbonate solids in suspension is recoveredby a solid liquid separation device (K), preferably a belt filter or apeeler centrifuge, and the resulting filter cake is washed, preferablywith de-ionized water (20). The washed lithium carbonate (21) is driedin a suitable drying apparatus (L) and then micronized according to sizespecifications in a milling device (M). The liquid stream (17)containing a mixture of strong and weak filtrate, also named washingwater, is sent to heat exchanger (0) where it is cooled (18), andsubsequently fed back to the vessel (F). A bleed stream of strongfiltrate (19) is sent preferably to solid liquid separation device (E)in order to wash impure lithium carbonate.

The bicarbonation process can be carried out batch wise or continuously.In the case of a continuous process, the bicarbonation reaction occursin a reactor or a series of reactors or a pipe-line reactor (G) whichensures a thorough mixing of the gas, liquid and solid phases. With theoperating temperatures between 10 and 40° C. the reactor is operatedpreferably between 8 to 15 atmospheres and when operating temperaturesbetween −15 and 10° C. the reactor is preferably operated at 0.7 and 8atmospheres. Similarly, the precipitation of pure lithium carbonate canbe carried out in one or a series of reactors (J) that can be operatedat a wide temperature range. The temperature used when precipitatinglithium carbonate in reactor (J) is higher than the temperature usedduring the bicarbonation reaction in reactor (G). The pressure used whenprecipitating lithium carbonate in reactor (J) is lower than thepressure used during the bicarbonation reaction in reactor (G). One ormore of the reactors (J) should preferably include strong agitationmeans to assist with the liberation of carbon dioxide. Operation of oneor more of the reactors (J) under vacuum or equally sparged with a gassuch as air, can also assist with the liberation of carbon dioxide gas.

Once the ion exchange resins are saturated they have to be regenerated.The regeneration involves first washing with water, then treatment withdiluted hydrochloric acid or diluted sulfuric acid to displace ions fromthe resin. The resin is then washed with water and regenerated withsodium hydroxide, potassium hydroxide or lithium hydroxide solution.

Spent hydrochloric acid or sulfuric acid solution used for regenerationof the spent ion-exchange resin becomes contaminated with both lithiumand calcium ions and can be recycled and used a number of times beforeit needs to be replaced and finally it can be sent to the concentratedwell brine in solar ponds in order to recover the lithium values.

Throughout this specification and the claims which follow, unless thecontext requires otherwise, the word “comprise”, and variations such as“comprises” or “comprising”, will be understood to imply the inclusionof a stated integer or step or group of integers or steps but not theexclusion of any other integer or step or group of integers or steps.

The reference in this specification to any prior publication (orinformation derived from it), or to any matter which is known, is not,and should not be taken as an acknowledgment or admission or any form ofsuggestion that that prior publication (or information derived from it)or known matter forms part of the common general knowledge in the fieldof endeavour to which this specification relates.

Those skilled in the art will appreciate that the invention describedherein is susceptible to variations and modifications other than thosespecifically described. It is to be understood that the inventionincludes all such variations and modifications. The invention alsoincludes all of the steps, features, compositions and compounds referredto or indicated in this specification individually or collectively, andany and all combinations of any two or more of said steps or features.

The present invention will now be described with reference to thefollowing non-limiting examples.

EXAMPLE I

A lithium containing brine was pumped from the well field of the Salarde Olaroz, located in Argentina. The brine was treated with slaked limein order to remove the magnesium as magnesium hydroxide with aco-precipitation of calcium sulfate. Subsequently the brine wasconcentrated in solar evaporation ponds until a concentration of 0.65%wt lithium/wt brine was obtained from the test facilities at Salar deOlaroz. Impure brine with 0.65% wt lithium/wt brine was used as startingmaterial for the lithium carbonate production at a lab scale accordingto the present invention. This brine was heated at 70° C. at 1 atm and a25% w/w soda ash solution was added to precipitate impure lithiumcarbonate. The impure lithium carbonate was filtered and washed withdeionized water.

The impure lithium carbonate was mixed with water and sent to a reactorwhere it was dissolved with a 30% excess of the stoichiometric amount ofCO₂ with respect to LiHCO₃ at atmospheric pressure and 18° C. in orderto produce an aqueous solution with dissolved LiHCO₃. The generatedsolution was filtered in order to remove the insoluble impurities suchas silica, iron, magnesium, calcium and boron compounds. The filteredsolution was split. One half was heated at 75° C. at 1 atm in order torelease the carbon dioxide and to precipitate Li₂CO₃, which wasfiltered, washed with deionized water and dried at 110° C.: The otherhalf was passed through ion exchange column with AMBERLITE™ IRC747 andsubsequently passed through ion exchange column with AMBERLITE™ IRC748in order to polish the solution and remove the final traces ofmagnesium, calcium and other dissolved ions. The solution was thenpassed through an ion exchange column with AMBERLITE™ IRA743 to removeboric acid and borates from the solution. The purified solution washeated at 75° C. at 1 atm in order to release the carbon dioxide and toprecipitate Li₂CO₃ which was filtered, washed with deionized water anddried at 110° C. Results for the impure and pure lithium carbonate ofthe test are showed in Table III

TABLE III Chemical analysis in weight percent. B % wt Ca % wt Mg % wtImpure lithium brine 0.460 0.007 0.016 Impure lithium carbonate 0.0500.292 0.047 Lithium carbonate without 0.002 0.041 0.774 Ion ExchangeLithium carbonate with Ion 0.0001 0.008 0.005 Exchange

EXAMPLE II

A lithium containing brine was pumped from the well field of the Salarde Olaroz, located in Argentina. The brine was treated with slaked limein order to remove the magnesium as magnesium hydroxide with aco-precipitation of calcium sulfate. Subsequently, the brine wasconcentrated in solar evaporation ponds until a concentration of 0.69%wt lithium/wt brine was obtained. This brine was used as startingmaterial for the lithium carbonate production process of the presentinvention. The results of chemical analysis of the concentrated brine isshown in Table IV.

TABLE IV Chemical analysis for lithium containing brine Chemical SpeciesBrine Content (% wt) Li 0.69 Na 7.73 K 4.05 Mg 0.001 Ca 0.018 B 0.382SO₄ 3.11

In the pilot plant, the brine was heated at 75° C., subsequently a 28%w/w soda ash solution was added in order to precipitate impure lithiumcarbonate. The impure lithium carbonate was filtered and washed withdeionized water. The impure lithium carbonate was mixed with cooledmother liquor from bicarbonation process. The slurry was heated to atemperature of 18° C. in a reactor (G) where it was dissolved with an20% excess of the stoichiometric amount of CO₂ with respect to LiHCO₃ ata pressure of 1 atm in order to produce an aqueous solution withdissolved LiHCO₃. The resulting solution with a temperature of 18° C.was filtered (H) in order to remove the insoluble impurities, such assilica, iron, magnesium and calcium compounds. Soluble or partly solubleions such as magnesium, calcium, other dissolved metals and boron wereadsorbed by selective ion exchange resin (I). The filtered solution witha temperature of 18° C. and at atmospheric pressure was passed throughion exchange column with AMBERLITE™ IRC747 and subsequently passedthrough ion exchange column with AMBERLITE™ IRC748 in order to polishthe solution and remove the final traces of magnesium, calcium and otherdissolved metals. The solution with a temperature of 18° C. and atatmospheric pressure was then passed through an ion exchange column withAMBERLITE™ IRA743 to remove boric acid and borates from the solution.The purified solution was heated at 75° C. in a strongly agitatedreactor (J) at atmospheric pressure in order to release the carbondioxide and precipitate Li₂CO₃ which was filtered and washed in a panfilter (K) with hot distilled water and then dried at 110° C. Thefiltered liquor was recycled back to the bicarbonation process. Resultsfor the impure and pure lithium carbonate of the test are showed inTable V.

TABLE V Chemical analysis for lithium carbonate Impure lithium Unitcarbonate Pure lithium carbonate Li₂CO₃ % 97.81 99.91 Na ppm 2200 7.6 Feppm 4.8 0.7 Ca ppm 3200 30 SO₄ ppm 2600 70 K ppm 540 1.1 Cl ppm 600 <50Mg ppm 370 8 Cr ppm <0.5 <0.5 Ni ppm <0.5 <0.5 Cu ppm <0.5 <0.5 Pb ppm<0.5 <0.5 Al ppm <5 <5 Zn ppm 0.8 <0.5 B ppm 680 <0.5 Si ppm 20 <10 H₂O% <0.5 <0.5 Insolubles in HCl % <0.5 <0.5 LOI (loss of % 0.1 <0.05ignition)

Example III

The bicarbonation process was conducted at different temperatures andpressures in order to define lithium bicarbonate solubility as functionof these parameters. Test T1 through T3 were each conducted under anatmosphere of CO₂ gas. T4 test was conducted at atmospheric pressure.T1, T2 and T4 were conducted at 20° C. and T3 at 6° C. T1 was conductedin a 2 litre stainless steel Parr autoclave. T2, T3 and T4 wereconducted in a 4 litre titanium Parr autoclave. The reaction slurry oftest T4 was sparged with CO₂ gas in glass reactor. In all samples a 10percent excess of lithium carbonate and CO₂ gas was added in order toassure the saturation of lithium bicarbonate. The reactors were operateduntil a constant pH was obtained. The test conditions are given in TableVI and the results are plotted FIG. 2.

TABLE VI Bicarbonation process test conditions Test Number Temperature(° C.) Pressure (atm) T1 20 5 T2 20 15 T3 6 8 T4 20 1

EXAMPLE IV

The solutions from said test T1-T4 in Example III were used as feedmaterial for the lithium carbonate precipitation tests from the lithiumbicarbonate solution by releasing CO2 gas. The tests were conducted in astandard 2 L Pyrex™ glass reactor. A wide temperature range between 20and 75° C. was tested. In order to improve CO₂ gas release, all testswere conducted with strong agitation, most of the tests with theexception of the T1a and T2a were conducted at a reduced pressure ofapproximately 0.4 to 0.5 atmospheres and at test T1a air sparging wasapplied. The bicarbonate solution of T4 was treated by an ion exchangestep with ion exchange resin IRC748 before being applied in test T4a.The test conditions are shown in Table VII and the lithium carbonatesolubility results are plotted in FIG. 3.

TABLE VII Lithium carbonate precipitation test conditions Solution fromResidence Test Number Test Temperature Conditions Times T1a T1 75 1 Atm.with air 4 sparging T2a T2 75 1 Atm. 4 T2b T2 20 reduced 6 pressure T3aT3 75 reduced 4 pressure T4a T4 50 IX - reduced 4 pressure T4b T4 50reduced 4 pressure

1. A method of producing lithium carbonate, comprising the steps of: a)precipitating impure lithium carbonate from an impure lithium containingbrine by addition of soda ash; b) reacting the precipitate of impurelithium carbonate in a first aqueous solution with CO₂ to form a secondaqueous solution containing dissolved LiHCO₃ and dissolved impuritiesand insoluble impurities from said impure lithium carbonate; c)separating said insoluble impurities from said second aqueous solution;d) separating said dissolved impurities from said second aqueoussolution by contacting said dissolved impurities with one or more ionselective mediums to remove said dissolved impurities wherein at leastone of the ion selective mediums removes boric acid and/or borates; ande) precipitating Li₂CO₃ from said second aqueous solution.
 2. The methodaccording to claim 1, wherein said lithium containing brine isconcentrated to approximately between 0.4% and 6.5% wt Li/wt brine. 3.The method according to claim 1, wherein said reacting step (a) to formimpure lithium carbonate from the lithium containing brine is carriedout at a temperature of approximately between 20 and 100° C.
 4. Themethod according to claim 1, wherein said impure lithium carbonate isseparated using a solid-liquid device.
 5. The method according to claim1, wherein said impure lithium carbonate is reacted with CO₂ at atemperature of between approximately −15° C. to 40° C. 6-7. (canceled)8. The method according to claim 1, wherein said impure lithiumcarbonate is reacted with CO₂ at a pressure between approximately 0.7atm and 20 atm.
 9. The method according to claim 1, wherein said impurelithium carbonate is reacted with CO₂ at a pressure betweenapproximately 1 and 8 atm at a temperature between approximately 0 and10° C.
 10. The method according to claim 1, wherein said impure lithiumcarbonate is reacted with CO₂ at a pressure between approximately 8 and15 atm at a temperature between approximately 10 and 40° C.
 11. Themethod according to claim 1, wherein said impure lithium carbonate isreacted with an excess of the stoichiometric amount of CO₂ with respectto LiHCO₃. 12-14. (canceled)
 15. The method according to claim 1,wherein said dissolved impurities include ions selected from the groupconsisting of Ca, Mg, Fe, Cr, Pb, Cd, As, Al, Ni, Cu, Zn, Mn, Si and acombination thereof.
 16. The method according to claim 1, wherein saidone or more ion selective medium is an ion exchange resin or fiber. 17.The method according to claim 16, wherein said resin or fiber has anaminophosphonic acid functional group.
 18. The method according toclaims 16, wherein said resin or fiber has an iminodiacetic acidfunctional group.
 19. The method according to claim 16, wherein a resinor fiber having an aminophosphonic acid functional group and a resin orfiber having an iminodiacetic acid functional group can be used inseries,
 20. The method according to claim 1 wherein said boric acidand/or borates is removed by an ion exchange resin or fiber having aN-methyl-glucamine functional group.
 21. The method according to claim 1, wherein said precipitation step (e) of lithium carbonate is carriedout at a temperature between approximately 20° C. and 100° C. 22-24.(canceled)
 25. The method according to claim 1, wherein saidprecipitation step (e) of lithium carbonate is carried out at a pressurebetween vacuum and 20 atm.
 26. The method according to claim 25, whereinsaid pressure is between vacuum and 1 atm.
 27. The method according toclaim 1, wherein said steps are carried out continuously or in batchmode.
 28. (canceled)